Processes for breaking petroleum emulsions



Patented July 1 1952 i f lT- 'Ii PROCESSES FOR BREAKING PETROLEUM IEMULSIONS Melvin De Gr-oote, University City, Mo rziss'ignor .to'Petrelite Corporation, Ltd., WilmingtcnrDeLv a corporation-hfflelaware "No'Draw'ing. pplication-A guste;1.950,

- *S'erial No. 177,554

ll-Glaimst (01. 252-331) This invention relates to; petroleum emulsions of the water-'in-oil type, that :are commonly referred to as cut oil, roily oil, ifemulsified oil, etc., and which comprise fine :droplets of naturally-occurring waters or brines dispersediin a more or'less permanent state throughout the oil which constitutes the continuous phase .of the emulsion.

One object ofmy invention is IOPIOVidBfiznOl/El process for breaking or resolving emulsions ::of the kind referred to.

Another object of my invention to provide an economical and rapid process for separating emulsions which have been prepared 'underacontrolled conditions from mineral 'oil, *such as crude -:oi1 :and relatively soft watersyor "tweak brines. aControlledemulsification and subsequent demu'ls'ification, under .the conditionsjust mentioned, are of significant value :in; removing impurities, particularly inorganic saltsifmm apipeline oil.

Demulsification, as contemplated in the present-:application, includes the preventive? step of commingling the demulsifier with lthe aqueous component whichtwould :orvmight subsequently becomeeeither phase of the emulsion; in absence of such precautionary :measure. :Similarly;.-'such demulsifier may :be' mixed 'with.:the hydrocarbon component.

Morespecifically, the:presentcinventionismoncerned with -a :process for :breaking {petroleum emulsions of the water-in-oil type, characterized by subjecting .the emulsion-to the action ;f..'certain oxyalkylated derivatives. ,The :particular oxyalkylated derivatives are obtainedyioyia process of '(a) Reacting a::phenol with :anialdehydeso as'toyield (b) .An oxyalkylation susceprtible,.ifusible, :organic solvent-soluble, "water-insoluble phenolaldehyddres'in; said resin being derived bywreaction between .al'difunctional monohydric phenoland an aldehyde having not over 8 .carbon atoms 2 and reactive toward" said phenol; -.said resin being formed i the substantialabsence of trifunctional phenols; said phenol being of the @formula:

2 said oxyalkylated resin :being characterized, :by theintroduction intoptheresin molecule :ofaa 1P1 rality :of :divalentwradicals f having :the formula B10, in which R c is::a;mem'ber selected from the class consisting :of .;ethylene radicals, propylene radicals, 'butylene radicals, lhydroxypropylene radicals, and hydroxybutylene;radicals; with -;the proviso that from'tabout ;one-half :to ,lessith'an two moles zofpalkylenerzoxide he introduced :for eachphenolic nucleus (d) Converting said oxyalkylated :resin -i into the corresponding-ualipyclic com-poundrbyi'hydroenation, .in presence hire hy o na ins a lyst;

(e) Reacting said rhydroaromatic compound with allyl ely idy .ethen-wth thewprovisoithatat least 2 moles ofallyl;\.glycidy1nether be reacted for each, alicyclic-molecule and not inexcess :of three times the number-of :hydroxyl radicals present in said molecule; g

(j) v:Polymerizing saidaallyl radical-containing derivative to .yield an organic solvent+s0luble product; and

(-g) subjecting ;said aforementioned Polymer to oxyethylation with (h) -Y-An al ha-beta al-kylene1oxide=havingrnot more than '4 carbon-atoms'andselected from the class iconsisting of ethylene .-,oxide propylene oxide, :butylene :QXide, islycide, and .-methylelyvcide :saidoxyalkylated resin zbeing characterized by the introduction into :thei-resin molecule 'ofwa plurality 0f divalent radicals having theiicrmula (-R10),v1in" whichaR z is a member selected from the 2 class consistingr-of- 'ethylene radicals,, -propylene radicalssbutylene radicals, lhydroxyprqpylene radicals,- and hydroxybutylene. radicals.

The oxyalkylated p0lymerized allyl-radicalcontaining hydroxylated I'BSiHSThQIGiII. described and used:- as demulsifiers for breaking waterinoilaemulsions, are 3prepared especially by a ;s ixstep procedure.

'(1) Theprepara-ti'on of;phenolaldehyde resins .:of :the kind described in detail in :U. :SJPQJLGIH? No. 2 499 370,- dated-March .Z, 1950; to=De Groote and Keiser, with the following qualification; Said aforementioned patent is limited .to resins obtained from .difunctional-tphenols havingv4'to 12 carbon atoms the:substituenthydrocarbon radical. .-For the present purpose the. substituent ;*may have asr'many asla-carbon atoms, aswinithe case-10f resins prepared ryfrom tetradecylphenol,

substantially para-tetradecylphenol. 'zlsimilarly,

resins 133111 the; preparedzfromhexadecylphenol or .octadecylphenol. This feature will-"he "referred to-subsequently.

(2) The .second step involves treating 211118 phenol-aldehyde resinso obtained with an 1kil ene r o'xidevselected from the {class of ethylen oxide, propylene oxide, butylene oxide, ralycide andmethyl lycidezin the ratio 10f at, leastnne and less than two moles of alkylene oxide per phenolic hydroxyl. The preparation of such derivatives is described in De Groote and Wirtel co-pending application Serial No. 99,361, filed June 15, 1949, now Patent No. 2,574,538, dated November 13, 1951. Said co-pending application illustrates the use of resins in which the hydrocarbon substituent in the rings may have as many as 18 carbon atoms, as previously referred to.

(3) The third step involves the hydrogenation of such oxyalkylated resins, i. e., the conversion of the aromatic compounds into the alicyclic analogues. The procedure employed is described in detail in co-pending application of De Groote and Keiser, Serial No. 64,443, filed December 8, 1948, now Patent No. 2,574,536, dated November 13, 1951. In said last mentioned co-pending application the phenols employed are selected from the same class referred to in issued U. S. Patent No. 2,499,370, -but needless to say, the process is equally applicable in the class of phe nols having as many as 18 carbon atoms in the substituent group, as previously described.

(4) The fourth step involves the treatment of the compounds in the presence of an alkaline catalyst with allyl glycidyl ether.

(5) The fifth step involves polymerization by means of a suitable reactant, such as an organic peroxide, or by oxidation of a gaseous oxygen-containing medium, such as air, or a combination of such procedures, or any other conventional procedure employed for producing polymers from conventional allyl radical-com taining materials. I

(6) The sixth and final step involves oxyalkylation by means of an alpha-beta alkylene oxide selectedfrom the class of ethylene oxide, propylene oxide, butylene oxide, glycide and methyl glycide.

The manufacture of resins containing both an allyl and a hydroxyl group are described in my co-pending application Serial No. 177,551, filed August 3, 1950, now Patent No. 2,574,817, dated November 13, 1951. The polymerization of such resins, for example, by drastic oxidation is described in my co-pending application Serial No. 177,552, filed August 3, 1950, now Patent No. 2,574,546, dated November 13, 1951. The oxy alkylation of such polymers is described in my co-pending application Serial No. 177,553, filed August 3, 1950, now Patent No. 2,574,547, dated November 13, 1951.

Reference is made to the following U. S. Patents: Nos. 2,499,365; 2,499,366; 2,499,367; 2,499,368, and 2,499,370, all dated March 7, 1950, to De Groote and Keiser. These patents describe phenolic resins of the kind herein employed as initial materials. For practical purposes, the resins having 4 to 12 carbon atoms are most satisfactory, With the additional C14 carbon atom also being very satisfactory. The increased cost of the C16 and Cm carbon atom phenol renders these raw materials of less importance at least, at the present time. Reference is made to Patent 2,499,370 for a description of the preparation of these resins, and to Examples 10. through 103a of that patent for examples of suitable resins.

The; specific examples of Patent 2,499,370 relate to resins derived from phenols having a substituent with 4 to 12 carbon atoms, but for preparing the products used in accordance with the present invention, the hydrocarbon substituent in the phenol may have as many as 18 carbon atoms, as illustrated by tetradecylphenol,

purchased in the open market.

4 hexadecylphenol and octadecylphenol, reference in each instance being to the difunctional phenol, such as the orthoor para-substituted phe nol, or a mixture of the same. Such resins are described alsoin issued patents, for instance, U. S. Patent No. 2,499,365, dated March 7, 1950, to De Groote and Kaiser, such as Example 71a.

As has" been pointed out previously, suitable resins can be made following the procedures previously described, or, for that matter, can be The second step in the overall process involves the use of an alkylene oxide, such as ethylene oxide, propylene oxide and glycide, or methylglycide. The most suitable oxides from an economical standpoint are ethylene oxideor propylene oxide. Obviously, the apparatus suitable for oxyethylation is also suitable for oxypropylation and will serve, if desired, for use with glycide.

I have prepared a large number of resins of the kind described above on a laboratory scale varying from a few hundred grams or less to somewhat larger amounts. Needless to say, they are also prepared regularly on an industrial scale. This same statement applies to the preparation of the oxyalkylated products with which this second part is concerned.

For a number of well known reasons, equipment, whether laboratory size, semi-pilot plant size, pilot plant size, or large scale size, is not, as a rule, designed for a particular alkylene oxide. Invariably, and inevitably, however, and particu larly in the case of laboratory equipment, the design is such as to use any of the customarily available alkylene oxides, i. e., ethylene oxide, propylene oxide, butylene oxide, glycide, epich1orohydrin, styrene oxide, etc.

Oxyethylations and oxypropylations are conducted'under a wide variety of conditions, not only in regard to presence or absence of catalyst, kind of catalyst previously described, but also in regard to the time of reaction, temperature of reaction, speed of reaction, pressure during re action, etc. Oxyalkylations can be conducted at temperatures approximating the boiling point of water, or slightly above, as, for example, 115 to 120 C.

Likewise, resins can be oxyalkylated, particularlywith ethylene oxide or propylene oxide, using temperatures and pressures which are comparatively high, for instance, temperatures in the neighborhood of 200 C., or in excess thereof, and pressures in the neighborhood of 200 pounds per square inch, or in excess thereof. Such oxyalkylations have been described in aforementioned U. S. Patent No. 2,499,370. Generally speaking, such procedure is employed under con:- ditions where there are more than three points of reaction per molecule and where the amount of oxide added is comparatively high in ratio to the initial reactant. Such procedure is entirely satisfactory in the particular oxyalkylation ste'p described herein.

However, since the amount of oxide is comparatively small, less than two moles per phenolic hydroxyl present in the resin unit, it is apparent that time is not a factor. In other words, it is just as satisfactory to employ a comparatively low temperature and low pressure rather than conditions of oxyalkylation previously mentioned, which result in rapid reaction rate. For this reason I have employed conditions of the kind involving temperatures of about to C., and pressures of 30 to 40 pounds, or less. If an atmosphere ofrinert gas, such as nitrogen, is

pounds gauge pressure.

accepts present during a reaction, needless tosay,- the pressures-may be'somewhathigher;

"Suchlow temperature, low reaction rateoxyalkylaitions have been described very completely in-UxS. Patent No. 2,448,664, to Fife et a1., dated September 7,1948.

As previously'indicated, low pressure, low temperature reaction ratesmay require considerable 'ti'me;as, forinstance, in some of the subsequent examples in the neighborhood of one to two hours. 'Actually, at 180 to 200 C., such reaction might be conductedin ten minutes or less. In large scale, low temperature operations the time might be somewhat longer, for instance, 5 to 8 hours. In any event, the reaction isso comparatively short that it is of no marked significanoe; but it' is more convenient to use these'lower temperatures on a laboratory or semi-pilot plant scale.

I have used conventional equipment with two added automatic features: (a) a solenoid-controlled valve which shuts off the propylene oxide in event the temperature gets outside a predeterminedand set range, for instance, 110 to 120 C., and (b) another solenoid valve which shuts off the propylene oxide (or, for that matter, ethylene oxide,'if it is being used) if the pressure gets beyond a predetermined range, such as '25 to '35 pounds. Otherwise, the equipment is substantially the same as is commonly employed forthis purpose, where the pressure of reaction is higher, speedof reaction is higher, and time of reaction is much shorter. For reasons which are obvious in'light of what has been said'previously, 'I have notfound it necessary to use such automatic controls under the conditions of oxyethylano employed in introducing such small portion of ialk'ylene oxide. Controls could be used, if desired, and certainly would be used in high temperature oxyalkylations.

"Thus, in preparing the variou examples, I have found it particularly" advantageous touse laboratory equipment which is designed to permit continuous 'oxyalkylation, whether it be'oxypropylati'on or 'oxyethylation. With 'certain changes, as will be pointed outhereinafter, the

"equipment can be used also to permit oxyalkyla- 'tion involving the use of glycide, where no pres- 'sure"i s involved except the vapor pressure of a solvent,if any, which may'have been used asa diluent.

'As previously'pointedout, the method of using propylenebxide is the same as'ethylene oxide. This point is emphasized only for the reason that the apparatus is so designed and constructed as to use either oxide.

"The oxyethylation or oxypropylation procedure employed in the preparation of the oxyalkylated derivatives has been uniformly the same, particularly in light of the fact that either a continuous automatically-controlled procedure 'was' employed, or else a short automatic method is 'used. 'Indeed, in this instance, the latter is preferred. In this procedure the'autoclave was a"conventional'autoclave made of stainless steel "and having a" capacity of approximately one gallonan'd' aworking pressure of one thousand This pressure obviously is far beyond any requirement, as far as ethylene or'propylene oxide goes; unless there is a reaction of explosive violence involved, due to accident. The autoclave'was equipped with the conventional devices and openings, such as the varithermocouple for mechanical thermometer; emptying outlet; pressure gauge; manual went line; charge hole for "initial reactantsjatleast one connection for introducing the alkylene oxide, such as propylene oxide methylene-oxide, to the bottom of the autoclave; along with suitable devices' forboth cooling and .heating the autoclave, such as a cooling jacket, and preferably, coils in addition thereto, with the jacket so arranged that 'it 'is suitable for heating with steam or cooling with water and further equipped with "electrical heating.-devices. -Such autoclaves are, of course, in essence, small-.-scale replicas of the'usual conventional autoclave used in oxyalkylati'on procedures. In some instances a larger autoclave was used, 1. -e., one'having-a capacity 'rang'ing 'in the-neighborhood 'of El i/ gallons.

"Continuous operation, or substantially continuous operation, was achievedby the use 'offia separate container to hold the alkylene "oxide being employed, particularly ethylene oxide 'or propylene oxide. The containerconsists-essentially of-a laboratory 'bomb having a capacity of about one-half gallon, or somewhat in excess thereof. In some instances, a largerib'ombwas used,-to'wit, one having a capacity of about-one gallon. "I'his bomb was equipped, also, with an inlet for charging and-an "eductor' tube 'going to the bottom of thecontainersoas to permit 'd-ischarging of alk ylene *oxide' in the 'liq'uid phase to th'e'autoclave. Other conventionalequipment consists, of course,'*of the -rupture disc, 'pressure gauge, "sight feed glass, thermometer connection for-nitrogen for pressuring bomb, etc. The bomb aldehyde' resin, one need not employ the automatic' devices unless desired. Autoclaves-of the nns described are equipped'with automatic controls {which would shutoff the-ethylene oxide or propylene oxide in the-event temperature of'reaction passes'out 'ofthe-predetermined range, or 'pressure 'in the-autoclavepasses out ofthe predetermined range. However, in procedure of the kind herein reported, I have "donenothing "fur- "ther than to set the inlet open sothe oxidewas added in a'pproximately two" hours and then'proceedto 'let the'autoclave run fora total of "three hours ,to insure completeness of reaction. Pressuresin-no instance registered more than"30"to 40 pounds and "the temperaturesvaried from One thing mu'st' be borne in-mind= when 'operating 'at' these comparatively low temperatures of oxyalkylation. 'When operating'at'a comparatively-high temperature, for instance, "between to200 C.,'an unreacted alkylene oxide,';su'ch 'as' ethylene or propylene oxide, makes itspresence felt in the increase in pressure orthe con- "sistency of a'high' pressure. However, at a low enough temperature it may happen that the oxide, such as propylene oxide, 80651111 as a'liq'uid.

If so, and if it remains unreactd; 'thersis. or

mantle.

course, inherent danger and appropriate steps must be takento safeguard against this possibility; if need be, a sample must be withdrawn and examined for unreacted propylene oxide, or ethylene oxide. One obvious procedure, of course, is to oxypropylate or oxyethylate at a modestly higher temperature, for instance, 140 to 150 C. Obviously, similar precautions are necessary in the case of ethylene oxide, although it is more reactive than propylene oxide.

I have found it comparatively simple to manually control the temperature of reaction by the use of cooling water, steam, or electrical heat to raise or lower the temperature. It will be noted the entire procedure herein involved is much simpler than where low pressure, low temperature, low speed reactants are employed in an effort to bring out the introduction of a comparatively large amount of alkylene oxide. Such procedure is sometimes used, for example, in treating diols or triols with ten to twenty or even thirty times their weight of alkylene oxide.

A word can be included in regard to the use of glycide. This is particularly pertinent, because a reaction involving allyl glycidyl ether, which reaction is also an oxyalkylation, broadly speaking, involves a reactant which is comparable to glycide. This is obvious, since glycide is 1 hydroxy-2,3-epoxypropane, and allyl glycidyl ether is 1-allyloxy2,3-epoxypropane. As previously pointed out, glycide is an alkylene oxide suitable for use in reaction with phenol-aldehyde resins. If either glycide or methylglycide is employed, no appreciable pressure is involved and no effort need be made to use equipment with automatic controls.

Indeed, in the use of a number of initial reactants with glycide, the entire equipment was used almost as if it were an ordinary piece of non-pressure laboratory equipment, since such reactions can be so conducted. Due to the high boiling point of glycide, one can readily employ a separable glass resin pot as described in U. S. Patent No. 2,499,365, dated March '7, 1950, to De Groote et al., and offered for, sale by numerous laboratory supply houses. Equipment of this kind has been advertised extensively in current chemical journals.

If such arrangement is used to prepare laboratory-scale duplications, then care should be taken that the heating mantle can be removed rapidly, so as to allow for cooling; or better still, through an added opening at thetop of the glass resin pot or comparable vessel should be passed a stainless steel cooling coil so that the pot can be cooled more rapidly than by mere removal of If a stainless steel coil is introduced, it means that the conventional stirrer of the paddle type is changed to one of the centrifugal type, which causes the fluid or reactants to mix, due to swirling action in the center of the pot. Still better is the use of a metal laboratory autoclave of the kind previously described above, but in elimination of external heat; and (c) the use of cooling, so there is no undue rise in temperature.

All the foregoing is merely conventional, but is included, due to the hazard in handling glycide. As to the use of glycide as an oxyalkylating agent, see U. S. Patent No. 2,089,569, dated August 10,

.1937, to Orthneret al.-

ethylene or propylene oxide.

The amount of catalyst used in oxyalkylatlori may vary from as little as /z up to 5. The amount may vary during the oxypropylation period, as exemplified by the addition of the catalyst at the very beginning of the reaction only and with no further addition. Needless to say, there is a comparatively high concentration of catalyst at the beginning of the reaction and a comparatively low concentration at the end; in fact, not infrequently the amount of catalyst at the end will be one-half of 1% sodium methylate, or caustic soda, or less. Catalyst can be added intermittently during the reaction period, provided suitable equipment is available. It is rather diflicult to employ such equipment on a laboratory scale, but it can be employed, or course, on a pilot plant scale or larger scale.

In the present situation, since comparatively little of the alkylene oxide was added per phenolic hydroxyl, time of reaction is not apt to be a factor. The amount of alkylene oxide may vary, for example, from one-half mole to less than two moles per phenolic hydroxyl. In other comparable oxyalkylations, as have been described in the literature, the amount of oxide added might be 50 to times this amount. Under such circumstances it is necessary to speed up the reaction in order to finish the process within a reasonable length of time. In the present case the amount of oxide added was so small that even using a low temperature (95 to C.) and a comparatively low pressure, less than 30 or 40 pounds maximum, the reaction was complete in a very short period of time. As a, convenience, I have generally added the oxide over a 3-hour period, since the apparatus was practically automatic. The amount of catalyst used was generally about 1.0% of the initial resin. Somewhat more can be used, or slightly less. If more is used, the reaction would, of course, be faster, and if less is used, reaction might be a little slower. It is my preference to use a minimum amount of catalyst, rather than an excessive amount, for the reason that it is desirable to neutralize the excess alkalinity with hydrochloric acid, for example, or sulfuric acid, or phosphoric acid, and remove the inorganic salt prior to hydrogenation.

One limitation of small-scale autoclave equipment (a gallon to a Z- gallon autoclave) is the difficulty involved in a suitable automatic device for adding a dry catalyst, such as sodium methylate, during the reaction. This presents no problem on a large scale with larger size equipment, and thus, the same operation conducted in equipment of increased capacity, means that all the catalyst need not be added at once, but can be added intermittently in a predetermined amount, based on an hourly rate, or based on the addition of For instance, in a large scale operation involving equipment having about twenty-five times the capacity of the autoclave employed, arrangements were made to introduce better than a gallon of ethylene or propylene oxide (4,000 grams) per hour, along with the introduction of 20 grams of sodium methylate hourly during the operation period. The net result, as far as'the final material was concerned, was the same, to wit, a residual alkaline catalyst equivalent to about /2 sodium methylate.

In the followin example sodium methylate is moles oi the phenol asa starting material. in

. poseof calculation the alkylene oxide added and the original phenol employed inmanufacture, was

used as a basis. This wasmore convenient than using. the weight of..resinobtained, because it, may vary somewhat from. batch to batch. Ac-- tually, the amountwas weighed on alaboratory balance, which mayhave been inaccurate to theextentof or ,45%; This, of course, is im material in' a procedure of the present type.

Similarly, the ethyleneoxide-and propylene oxide.

were weighed as closely as possible, but here again the variation couldhave beenpff. to provide theresin. The amount ofxoxides em? ployed are shown in the table.

S grammoles of the phenol were usedto The amount of catalyst (sodium methylate) employedis also.

shown. In all instances the temperature; as-

stated, was never higher than. 115 (Land gener; ally varied from 100 to 110 C. The pressure was never higher than 40 pounds per squareinch, and in: all instances; the reaction was complete in three hours.

Oxyethylation or oxypropylation was conduct-.

ed in the usual manner, first sweeping out the equipment with nitrogen and setting the controls as far as-the additionzofthe oxide Wasconcerne-d, but ignoring the controls as far as temperature and. pressure were concerned. Any adjustment requiredsin the matter of temperature-and 'pressure" could" bemade manually by'examination of 486 grams. ofa resin of the kind.:describedas complete.

for each initial phenolic hydroxyl involved in; resinv manufacture.-

Example 1a of Patent 2,499,370 mixed with 300 grams of xylene, were used as the initial charge. 'Iothis there was added about 1% (5 grams) of sodium methylate. These ingredients were placed 7 in the autoclave and the autoclave sealedand the. automatic devices adjusted for injecting a comparatively small amount of oxide, 135 grams, in about 2% hours. The reaction was continued for a'itotal of 3 hours, however, to besure it was.

This is a, ratio of one mole otoxide- The temperature was ap proximatelyl10 C. and the pressure was less than 30' pounds per square inch. The finalprod not was a viscous, semi-resinous product, being;

somewhat between a resin and a viscousambercolored ifiuid obtained by increased ioxyethylation In such instances where the resins employed were liquids, needless to say, further oxyalkylation was; in the direction of reduced viscosity. Some-resins which were practically viscous liquids to start. with, beeameless viscous or moretowards-the .liquidstage The color varied from deep red of,

amber in some darker shades, and in someine stances, lighter shades. The residual product was, ofrcourse', slightly alkaline.

For. the purposedesoribed in the; next succes sive part, each particular sample wasneutralizedf with hydrochloric acid and. then the xylene;- eliminated by vacuum distillation. The resin or tacky resinous liquid, or liquids, so obtained, was then dissolved: in ethyl. alcohol and filtered. to remove any inorganic salts. 'The xylene-free; alcohol solution was used for hydrogenation.

The following table illustrates a variety of suitably oxyalkylated resins." Such resins can be treated,"of"course, with glycide inexactlythe sam'emanner under the same conditions, with. the. exception that the. autoclave, is simply used as a reaction. vessel withaicondenser and with,- out theuse-ofpressure. However, in. handling glycide, I. prefer touse the glass resin pot in the manner-previously described. Glycide reacts very rapidly-and-themolecular proportions, etc., are within-the limits, previously. specified.

In:. column. 2; the resinsgare identified injterms of the example number of Patent 2,499,370.

No. of Gr.

Ratio Moles Grs. 0i M01. Amt.

Ex. Orig. Grs. Mol. Max. Resin Oxide to Catalyst of Max. Pres. Ex. No. No.91 Xylene Phenol ETO Equiv- Phenolic Emp1oyed can Tgimp. inch Time in hours i RBSIIL Repre- Used alent. w 0.

Solution sented by Hylyst Solution droxyl la 786 3 135 3- 1:1 sodium-methylate; 5 Up to 40lbs... 3 hrs. or less. lo 786 3' 200 4% d 5 do Do. In 786 3 235 5%. 6 D0, 311 828 3 135 3* 6 Do. 30' 828. 3 200' 4% 6 D0. 311 828 3- 235 5% 6 Do. 7a 870' 3' 135 3 6 .130. 7a 870 3 200 4% I 6 Do. 7a 870- 3 235- .5% 6 D0. 811 954 3 135 3 7 D0, 811 954. '3 260 4% 7 Bo. 8a 954 a 235 554. 7 Do. 9a 846' 3 135 3 6' D0, 9a 846 200 4% 6 Do. 911 846 3 235 5% 6 Do. 690' 1; 032 3 135 3 7 D0. 69!: 1, 032 3 200 4% 7 Do. 6911 1,032 3 235 5% 7 Do. 70!! 996 3 3 6 Do. 70a 99a 3 200 4% a Do. 70;: 99s 3 235 5% 6 Do. 70a 1,038 3 135 3 7 D0. 70a 1, 038 3 200 4% 7 Do. 7011 1,038 3' 235 5% 7 Do. 73a 1,122 3 135 3 8 DO. 7311' 1,122 3 200 4% g 8. Do. 7311' 1,122 3" 235" 5% 8 Do. 14a- 810 3' f 135 3" 5' Do.

No. of Gr Ratio Moles Grs. oi Mol. Amt Ex. On". Grs. M01 Max 4 Rosin Oxide to Catalyst of Max. Pres. 13x. No. No. of Xylene Phenol ETO Equiv- Phenolic Employed Oata Temp. per inch Tnnoin hours Resin Solution Repre- Used alent H 1 St 0.

sented by g 1 y Solution y 14a 810 3 200 4% 1%:1 sodium methylate. 5 95-115 Up to 40 lbs.-- 3 hrs. or less. 1%11 g 3% 1%:% -d 95-115 go. a 5 o. 141 786 3 260 4% 13411 5 D0. 141 780 3 305 5% 1%:1 5 Do. 828 3 175 3 1:1 6 D0. 3a 828 3 260 4% 13621 6 D0. 3a 828 3 305 5% 1%:1 6 Do. 741 870 3 175 3 1:1 6 Do. 7a 870 3 260 4% 1%:1 6 Do. 711 870 3 305 5% 1%:1 6 D0. 811 954 3 175 3 1:1 7 D0. 811 954 3 260 4% 1%:1 7 Do. 811 954 3 305 5% 1%:1 7 Do. 7211 1, 038 3 175 3 1: 7 Do. 7211 1, 038 3 260 4% 1%:1 7 D0. 72a 1, 038 3 305 5% 1%:1 7 Do. 730, 1, 122 3 175 3 1:1 8 Do. 73a 1, 122 3 260 4% 136:1 8 Do. 73a 1, 122 3 305 5 1%:1 8 Do. 14a 810 3 .175 3 1:1 5 D0. 1411 810 3 260 4% 1%:1 5 Do. 14:: 810 3 305 5% 1%:1 5 D0. 24a 1, 062 3 175 3 1:1 7 D0. 24a 1, 062 3 260 4% 1%:1 7 D0. 24a 1, 062 3 305 5% 1%:1 7 Do. 34a 843 3 175 3 1:1 5 Do. 34a 843 3 260 4 /6 1%:1 5 Do. 34a 843 3 305 5% 1%:1 5 Do. 800 1, 365 3 175 3 1:1 10 Do. 8011 1, 365 3 260 4% 1%:1 10 D0. 8011 1, 365 3 305 5% 1%:1 10 Do.

The following examples illustrate the hydrothe gauge pressure in pounds per square inch and genation of the oxyalkylated resins.

Example 10 The oxyalkylated resin was the one previously identified as Example lb. This product, as prepared, contained xylene and a small amount of basic catalyst. Enough concentrated hydrochloric acid was added to neutralize the basic catalyst. As previously noted, the xylene was removed by vacuum distillation at a temperature not in excess of 200 C. During the removal of the xylene, the water introduced by the addition of a small amount of hydrochloric acid was also eliminated together with any small excess of hydrochloric acid which may have been present. This residual material was then dissolved in 300 grams of ethyl alcohol, 1. e., an amount equal to the xylene originally present. The anhydrous ethyl alcohol solution was allowed to stand for three days and then filtered so as to remove a small amount of precipitate. The amount of solution at this time was substantially the same as at the end of the previous operation, to wit,

approximately 921 grams, of which 300 grams represented solvent. This was hydrogenated. in two substantially equal half portions. Approximately 460 grams of the material described were placed in an autoclave along with 31 grams of Raney nickel. The amount of Raney nickel used in all instances was approximately 10%, by weight, of oxyalkylated reaction calculated on a solvent-free basis. 7

The apparatus employed was a stirring type super-pressure autoclave manufactured by the American Instrument 00., Silver Spring, Maryland, and described in their catalogue No. 406 as the 4%" series. The instrument was, of course, equipped with all the conventional fittings. The stirring speed employedwas approximately 450 R. P. M. The following table shows the time required to hydrogenate. The initial time period shows the starting period in the morning and the second and third columns show the temperature in degrees centigrade:

Pressure Temperaature C.

The next morning, after standing overnight, the temperature had dropped to 26 C. and the pressure to about 835 pounds. The material was then removed by draining the autoclave and then washing with approximately 400 to 500 grams of anhydrous isopropyl alcohol. The mixture of alcohols was then removed by vacuum distilla tion at less than C. The hydrogenated product was substantially identical in color as prior to hydrogenation, although there may have been some bleaching effect during the hydrogenation reaction. The solubility of the material was not particularly changed in comparison to the prod.- uct prior to hydrogenation. The tests for aromatic character, such as deoolorization of bromine Water, indicated that the product was entirely, or nearly entirely converted into a hydroaromatic compound.

Similar hydrogenation was conducted in which no alcohol was employed as a solvent, the resin having been added to the autoclave in a powdered form, and in such procedure the temperature of the autoclave was raised to C. before startaeoaosz sure, particularly at the higheroperating' tern-e peratures.

The same procedure was carried. out'in. regard to -allfthevarious oxyalkylated productszdescrihed above. The following table: shows the; example number-correspondence between the oxyethylatedi non-hydrogenated material and: the derivative obtained by hydrogenation, together with the maximum temperature, pressure, and time em.- ployed in hydrogenation. In each. instance; the amount of catalyst. employed. (Raney nickel) was approximately %"of the solvent-free powder. In some instances, low'molal alcoholswere employed assolvents, and in other instancesno solvent was present. Actually, the hydrogenation procedureusing Raney nickel and equipment of" the kindtnow available is comparatively simple.

Inthe matter'of hydrogenated phenol-aldehyde resinsseel U. S. Patents 2,072,142 and 2,072,143, both dated March 2, 1937; and both to Ubben.

1 Astochange: in: physlcalappearanceas a result. offhydrogenation; attention .is;.directed;to:v what has. been. said. preceding; Hydrogenation .nu.- merous. cases; does show some. bleaching; efiect.

The. hydrogenatedqproduct freedfrom solvent which would be susceptible to. reaction withglyciw dylz "allyl. ether; was: admixed. with approxizmately 30.0. grams of:;xylene and approximately 1% ofsodiummethyl'ate. Needless to say, the alcoholemployed: as. azsolvent, and-for that. mat ter, the :xylene: employed as a solvent; produceing the initial resin,; could. be. replaced'by-a: sol-. vent which wouldinot be objectionable eithenfrom a -standpoint. of hydrogenation or .oxyalkyl'ation, as, for example, decalin; Again, as: has, :'-been pointed out, all the reactions. involvedcanybe conducted in absence of any solvent. purely a matter oi convenience.

In noting the size of the batchsubjectedytoa reaction with allyl. glycidyl ether, noaocount is.

taken for; increase in weight, due to. hydrogena: tion, for the-reason that this is a comparatively small factor and there have been. some losseszin filtering, and otherwise. Therefore, therfigures that follow: correspond in essence to. the figures appearing in Table II, which show" the grams of xylene solution, plus the oxide added. Actually, the treatment with allyl glycidyl ether, as previously noted, is an oxyalkylation. process and :the' reaction is conducted in the same manner. as previously mentioned and is substantially the same as one would conventionally employ inthe use of glycide.

As previously indicated, the next. step is thereaction betweenallyl glycidyl ether and theali cyclic compounds obtained. in the. manner described above. Such alicycliccompounds are poly-hydroxylated, having at least three or more hydroxyl radicals per molecule. Generally speakeing, the number of hydroxylradicals, if obtained by the reaction-of ethylene oxide or propylene oxide, for example, would run from 3 to 7 or 8, unless the resin, prior to hydrogenation, had been treated in such a manner as to have present a greater number-of. phenolic. hydroxyls, such as a condensation reactionto increase the resin molecule size. Obviously, if glycide or methylglycide were used, thenumber of hydroxyl. radicals would be substantially larger, for instance, 10., 15, 20 or even more. In any event, the amount of allyl glycidyl'ether employed is sufiicient to convert at least a plurality of hydroxyl radicalsper molecule intothe corresponding allyl compound and may be enough. to convert allhydroxyls present, or two or three times this molal amount. More allyl glycidyl ether can be-employed than correspondstothe. molal proportion, based onhydroxyl radicals present, for the simple reason that at each stage ofreaction a, hydroxyl is-obtained which, in turn, is susceptible to further oxyalkylationwith any alkyleneoxide, and of course, with allyl glycidyl ether.

The use of allyl glycidyl ether, as previously noted, involves substantially the same, procedure and equipment as glycide. The glass equipment previously described could be used, although I have found itrmore convenient to employ the Time of. ExuNo: of Hydra Ex; No. of Max. M ax. Pres. genatecl. Deriva- Oxyalkyl- Temp. lbs. per 1 tive ated Resin 0. square inch H ours 1b 240 1, s70- 13 2b- I as) 1, 83.0 6 3b 260 1, 7901 5% 4b 245 1,815- 5b 250' 1, 890 6b 260. 1, 835 5%. 7b 240 1, 795 =1 3 8b 235 1, 800' 6% 9b 230 1, 730 63. 10b 250 1, 725 Ht 245. 1,750 5 1217 240 1, 725 7 135 240 1, 800 6% 14b 230 1, 325- 1 15b 235 1, 830 7% 16b 245 1', 850 7 1?!) 255 1, 790 6 4 181) 1 250 1, 820 5 /4 191) 260 1', 890 5%, 20b 255 1', 835 5% 21b 245 1, s20 1 221) 240 1, 815 7%- 23b 240 1', 850, 7 24b U35 1, 825 6%" 255 235 1, 830 8 26!) 250 1', 750 7 /2 275 Y 255 1', 765' 7% 28!) 245 1', 765 6 /1 29b 240 1, 780 5% 305 260 1, 890 6 3]!) 266 1, 800 5 32b 235 1, 805 6% 3317 255 1, 790 7 34b 1 255 1, 780 7% 351) 240 1', 725 5311p 360 240 1, 725 6' 3711 235 1, 830 5% 3st 245 1, 820' 6% 301) 260 1, 880 6% 401) 230 1, 795 7 41!) 250 1, 725 7% 421'? 240 1, 800 7% 430 245 1, 790 5'34 441) 260 1, 820 612' 43!) 265 1, 835 5 461) 250 1, 850 5% 47b 255 1, 815 6 4% 240 1, 790 6 14' 495 230 1,750 (ll- 50b 2 60 1, 890 5%- 51!) 240 1,850 i 7% 520 245 1, 730 7 53!) 240 1', 855- 6% 5417. 255 1', 770 V 7% 55b 235 1, 840 5 56!) 230 1, 890 5% 571) 255 1, 755 6% 585 255. 1, 835' 6% 59!) 240 1, 860 71 60b 250 1, 820 7% 61b 250 1,850: 8% 62b. 24D. 1, 795 8..

larger laboratory autoclave previously, described.

The, use. will be illustrated by the following examples.

. Emmple. 1d

The, same piece of equipment wasemployed as previously described, i. e., an autoclave, although in the instant procedure involving the use of allyl glycidyl ether, there was no pressure involved and certain changes were made, as noted subsequently. The autoclave was equipped with a water-cooled condenser which was shut ofr when used as an autoclave. It was equipped also with a separatory funnel and an equalizing pressure tube so the liquid, such as allyl glycidyl ether could be fed continuously at a drop-wise or faster rate into the vessel, and the rate was controlled by visual examination. For convenience, this piece of equipment is referred to as an autoclave, because it is essentially designed for such use. butit is to be noted it is not so used when allyl glycidyl ether, or for that matter, glycidol, was employed as described above.

There were charged into the autoclave 921 grams of a xylene solution (containing 300 grams of xylene) identified as Example 10, preceding. Such amount of sodium methylate equivalent to about 1 of the hydroxylated reactant was added as a catalyst, which, in this instance, was 6.5 grams. The autoclave was sealed, swept with nitrogen gas and stirring started and heat applied immediately. The temperature was allowed to rise to 123 C. The allyl glycidyl ether employed was the technically pure product.

The hydroxylated reactant present in the autoclave represented approximately 3 moles of phenol when calculated back to the initial reactants. The amount of allyl glycidyl ether added was approximately 3 moles or 350 grains. This was added over a 3 /2 hour period. This Was charged into the upper reservoir vessel which had been flushed out previously with nitrogen and was, in essence, the equivalent of a separatory funnel. The oxide was started slowly into the reaction mass at a drop-wise rate. The reaction started immediately and the temperature rose approximately 13 to 19. Cooling water was run through the coils so the temperature for the addition of the oxide was controlled within the range of 16 to avoid any possible entrance of air. Under such operation there was, of course, some loss of xylene, but examination revealed no loss of the oxide.

The product, so obtained, was fluid, lighter in color than the initial example, and on examination, was found to be comparatively free from unreacted oxide. Likewise, examination by determination of the hydroxyl number showed sub-. stantial completeness of reaction. Needless to say, such procedure also increased the water. solubility of the product.

What is said inv this instance in regard to physical properties applies, for all practicalfpurposes, to all examples obtained. Obviously, where increased amounts of the ether were employed, the final product tended to show more and more the characteristics of a viscous liquid comparable to castor oil or slightly blown castor oil. The

color alsodecreased as more oxide was added.

Example 203 The same procedure was employed as in Example 1d, preceding, using the same operating procedure and substantially the same temperature range, with this clifierence: the product subjected to treatment with allyl glycidyl ether was the hydroxylated compound identified as Example 2c, preceding. The amount employed in this instance was 986 grams, including 300 grams of solvent. The amount of sodium methylate used as a catalyst was 7 /2 grams. In all other respects E N r 1 r gfi x. o. o Icyc 1c A t o to M Alicyclic Cmpd. Amt. Amt. m each Mole Temp Tlme No Cmpd Used (sol- Solvent grs. Catalyst grs. E Phenolgi Used vent-free g Originally eactwn actlon basis) grs. present 621 300 Sodium methylate. 6. 5 350 1:1 Not over 138 1 686 300 7% 350 111 138 721 300 .(10- 7% 350 1:1 138 2% 789 8 350 1 :1 138 4 854 9 350 1 :1 138 3% 889 -4110..- 9 350 1:1 138 3% 867 ..--(10- 9 350 1:1 138 3 932 do. 10 350 111 13a 2 967 ...(10- 10 350 1:1 138 4 957 d0 10 350 1:1 138 41 1,022 (10 10 350 1:1 138 4% 1, 057 do 11 350 1:1 138 3% 621 do 7 350 1:1 138 2% 686 (10 7 250 3:4 138 2% 721 (10-- 7 260 324 138 2 789 "J10-.." 8% 250 324 138 3 854 d0. 9 260 3:4 138 3% S89 "J10-.. 10 260 3:4 138 4% 867 d0 9 260 324 138 4 932 (10.. 916 260 324 138 4% 967 (10 10 260 3:4 138 3% 957 (10u 10 260 3:4 138 4 1,022 .(10- 10 260 324 138 4% 1,057 .d0 11 260 3:4 138 3% 745 d0 3 350 1:1 138 3% 830 "410--" 9% 350 1:1 133 4 875 ..d0 9 350 1:1 138 3 /5 685 110....-- 7 350 111 138 3 770 .(10 3% 350 1:1 138 3% 815 (10- 8 350 121 138 2% to C. The reaction took place at atmospheric pressure with simply a small stream of nitrogen passing into the autoclave at the very top, and passing out of the open condenser so as Attention is again directed to the fact that other suitable solvents other than xylene may be used, such as decalin, cymene, etc. Other 75 suitable catalysts can be employed. It is also pointed out that the amount of allyl glycidyl ether employed need be only enough to introduce a plurality of allyl radicals per resin molecule, or may be enough to introduce-a number of allyl radicals equal to the original phenolic hydroxyls, or twice as many, or three times as many. My preferred ratio is to use 3 moles of allyl glycidyl ether for each 4 moles of phenol originally used, or to use an equal number of moles, 4 for 4, or else 5 moles of allyl glycidyl ether for each 4 moles of phenol originally used.

The allyl radical-containing products are polymerized in much the same way as oomparable products, for instance, castor oil, dehydrated castor oil, allyl sucrose, or the like, are polymerized or thickened or bodied. Such polymerization is due essentially to the allyl group's undergoing allyl or vinyl condensation, or polymerization. Such viny polymerization is usually induced by use of a peroxide catalyst, such as benzoyl peroxide or blowing with a gaseous oxygen-containing medium, or by using a combination of the two procedures.

In any event, the usual steps are taken to free the compound from any solvent, such as xylene, which may be present and also to render it as nearly neutral as possible and to remove any inorganic salts which would tend to separate out. A slight basicity, due to the presence of a basic tertiary amine, is desirable in connection with the use of a peroxide. ihis applies whether the peroxide is used for partial polymerization, followed by blowing withair, for example, or is responsible totally for the polymerization. This practice, i. e., the use of a tertiary amine to act as an activator in peroxide, for instance, benzoyl peroxide, to induce polymerization is well known. Tin chloride seems to have similar properties, but is not as satisfactory. For a number of reasons, omdation by means of air alone seems to be the simplest and the most satisfactory procedure.

Briefly stated then, the various products identified as Examples 1d through d, preceding, are neutralized with suflicient concentrated hydrochloric acid to make them neutral. Any sodium chloride formed is removed by filtering. The. product is then subjected to vacuum distillation which removes the xylene used as a solvent and also any water formed during the neutralization step. The final product varies from a semi-viscous liquid to a viscous or tacky liquid, or a product which exhibits almost a solid state at ordinary temperature. In all instances these products are fluid at the temperature employed for polymerization, for instance, 110 to 150 C; Previous reference has been made to the fact that polymerization with air is comparable to the procedure that is used in obtaining an oxidized oil or blown oil, or a polymerized castor oil from castor oil or similar materials, as, for example, allyl sucrose. Such products are produced by the common practice of blowing or oxidizing the polymerlzable material by means of a gaseous medium, such as air, oxygen, ozone, or ozonized air. The gaseous medium, such as air, may be moist or dry and the oxidation, or better still, polymerization, may take place in presence or absence of a catalyst. The catalyst may be of a metallic type, such as lead ricinoleate, cobalt ricinoleate, manganese ricinoleate, etc., or it may be of an organic type which produces a peroxide, such as alpha pinene, linseed oil, etc. Similarly, as previously noted, peroxides themselves, such as benzoyl peroxide, or similar peroxides, may be employed as catalysts or to initiate the incipient stage of polymerization. Such peroxide catalyst may be used in presence of a basic tertiary amine, as previously noted. The amount of catalyst may vary from as little as one-tenth of l to 1%, or somewhat less. The amount of tertiary amine employed in connection with the peroxide is usually in approximately the same order of magnitude, i. e., one-tenth of 1% up to 1%. Examples of such tertiary amines include tributylamine, triamylamine, tricyclohexylamine, etc.

Polymerization can be induced by oxidation at atmospheric pressures or superatmospheric pressures, i. e., pressures up to or including 200 pounds gauge pressure, and at temperatures from slightly above the boiling point or" water, up to any temperature that does not produce undue decomposition by pyrolytic reaction.

The time of polymerization, as induced by blowing or oxidation, may be fairly brief, for example, less than 25 hours, particularly if such oxidation takes place in conjunction with the use or" a peroxide, such as acetyl peroxide or benzoyl peroxide. On the other hand, in some instances, using a temperature of approximately C'., it is sometimes necessary to blow the mixture for as long as 125 to hours.

Not infrequently there is a change in the index of refraction of products during the polymerization stage. In other words, as the allyl radicals disappear, due to polymerization, there is an increase in the index of refraction. Under any particular set of conditions a study of such index of refraction may be helpful in controlling the polymerization, although as a rule, viscosity is equally satisfactory insofar that no effort is made to reach an exact quantitative point in the polymerization range. Generally speaking, I have attempted to prepare compounds having at least three different degrees of polymerization. One stage is where there has been a noticeable increase in viscosity and the difference is substantially comparable to the difference between heavily blown castor oil and ordinary castor oil; the second stage is the point where the product begins to show incipient stringiness. This is probably where incipient gelation or cross-linking starts to take place. The third stage is where stringiness is not only obvious but a solution of the polymerized solution in xylene, for instance, a 50% solution, still shows stringiness but is still soluble. It is to be noted that the ultimate product, whether below the stringy stage or in the incipient stringy stage, or at the stage where even a 50% solution in xylene is stringy. must be soluble in an organic solvent, such as xylene, low molal alcohols, decalin, diethylether of ethylene glycol, cyclohexanal, or the like. If the product is not soluble in any one of the common hydrocarbon or oxygenated solvents, it is not satisfactory, for the herein described process.

Polymerization is illustrated by the following examples:

Example 1e A product of the kind identified as Example 1d above was freed from inorganic solvents and salts. The product was substantially neutral. 1500 grams of the product were placed in an ordinary S-liter flask. The air terminal inlet was provided with a device which gave a multiplicity of small, fine bubbles. This was accomplished'by means of a porous ceramic tube fitted to glass and available from various laboratory supply houses. The imput of air was such that there was a continuous stream of air passing through is the reaction mass sufiicient to provide at least moderate agitation. The temperature was raised to 138 C., and then air was passed through for 117 hours. During approximately the first third of the period, i. e., for the first 40 hours, there did not seem to be any particular change.

During the second 40 hours the material began to darken and wa almost blackish-red at the end of 80 hours. By this time there was a modest but appreciable change in viscosity, even though not so marked as at the end of the final reaction period. Viscosity, of course, could not be judged satisfactorily when the material was hot, but when the reaction mass was allowed to cool and the viscosity compared with that of the initial reaction mass at the same temperature, for instance, room temperature, it was obvious that a thickenin somewhat suggestive of the change that takes place when castor oil is converted into a light blown castor oil, had taken place.

At the end of the final period the viscosity of the product had greatly increased and was suggestive of that of heavily blown castor oil. The initial product showed a viscosity more comparable to ordinary castor oil. This product was considered a characteristic as being the result of mild blOWil'lg or mild polymerization. Note what is said in regard to such characterization in subsequent Example 'le.

Example 2e The same procedure was followed in every way as in Example 16, except that the initial charge was 1500 grams of a product identified as Example 2d, preceding. The temperature of polymerization, the time period. the change in the product, change in color, final viscosity, etc., were substantially comparable to Example 1e, precedmg.

Eaample 3e The same procedure was followed in every way as in Example 1e, except that the initial charge was 1500 grams of a product identified as Example 3d, preceding. The temperature of polymerization, the time period, the change in the product, change in color, final viscosity, etc., were substantially comparable to Example 1e, preceding.

Eacample 4c The same procedure was followed in every way as in Exampel 1e, except that the initial charge was 1500 grams of a product identified as Example 28d, preceding. The temperature of polymerization, the time period, the change in the product, change in color, final viscosity, etc., were substantially comparable to Example 1e, preceding.

Example 5e The same procedure was followed in every way as in Example 1e, except that the initial charge was 1500 grams of a product identified as Example 30d, preceding. The temperature of polymerization, the time period, the change in the product, change in color final viscosity, etc., were substantially comparable to Example 1e, preced ing.

Example 7e The same procedure was employed as in Examples 1e through 6e, preceding, except that a stirring device was included in the reaction flask along with the distributing unit. In this case the temperature was held at slightly less than in the previous six examples, i. e., at about 136 C. The stirring device apparently gave better oxidation, which, in turn, resulted in more effective polymerization. At the end of the hours the product was not only stringy, but when mixed with an equal weight of xylene, the 50% xylene solution, so obtained, showed stringiness. In fact, the product, prior to dilution in xylene, was even more than stringyit was somewhat rubbery. I have characterized the product which is blown just short of the rubbery or stringy stage, as exemplified by Examples 1e to tie, preceding, as being mildly oxidized or mildly blown, or mildly polymerized.

I have used the expression drastically oxidized to indicate a product which is not only stringy or rubbery as such, but also is highly viscous and shows stringiness or rubberiness in the 50% xylene solution. Such stage is typified by the present example, i. e., Example 7e.

Examples 8e to 12:

Example 13e The same procedure was employed in every respect as in Examples 1e through 7e, preceding, and the particular procedure employed was the use of the stirring device, as described in Examplele. The initial charge as before was 1500 grams of the product identified as Example 1d. The temperature of polymerization was again within the range of to C.

In this example, and in the subsequentfive examples, the time period was less than in Examples 7e to 12c, inclusive. In the instant example it was 82 hours. This product at the end of this period showed a definite tendency to string or rubberize, but this property practically disappeared when a 50% solution in xylene was prepared. I have referred to this particular stage as being semi-drastically oxidized to indicate a.

product which shows incipient stringiness, as such, but where such stringiness disappears on dilution, as previously noted.

Examples 14c to 18c, inclusive The same procedure was followed as in Example 13c, preceding, 1. e., a procedure employedso as to produce a semi-drastically polymerized product and the products subjected to polymerization were identified as Examples 211, Bel, 28d,

29d, and 30d, preceding.

Actually blowing or polymerizing can be conducted with ozone or ozonized air, as well as airwhich may or may not have its moisture content eliminated. In this particular type of reaction I have found no advantage in going to any added;

cost in regard to the oxygenating'procedure which initiates polymerization.

' The same is true of a catalyst, such as lead, manganese or cobalt naphthenate or the like, as has been described in the literature previously mentioned. Such catalyst in comparatively small amounts, one-tenth percent or preferably less, will speed up the polymerization, but here again I have not found this particularly desirable. Since it is usually intended to stop the polymerization at some particular point by use of a mild blowing or semi-drastic blowing, or a drastic blowing, it is of greater convenience to approach the .end point slowly, rather than rapidly, and also to have polymerization cease when the air stream stops.

As I have pointed out previously, the period of oxidation can be controlledin various ways; for instance, a higher temperature can be used or more air will be forced through the mass; more violent agitation can be employed; and most important of all, if desired, one can shorten the so-called incubation period by use of a peroxide alone or a peroxide in combination with a tertiary amine. My experience indicates that in many instances there are present materials which appear to inhibit the polymerization step, possibly a trace of phenolic compounds. Oxidation appears to counteract or destroy these products slowly and then an incubation period seems to develop where peroxide, or the like, is built up. After this stage, polymerization takes place comparatively rapidly. This conforms to the pattern of other comparable polymerizations involving allyl compounds. I have been able to cut down the time required in preparation of products characterized byExamples 1e through 18c, preceding, by doing nothing more than adding about of benzoyl peroxide and blowing until incipient viscosity change takes place. If this did not appear in the first ten hours, I then added a second equal portion of benzoyl peroxide and repeated. Usually, the first addition of benzoyl peroxide or a slightly larger amount was sufiicient. In some instances, I have made an addition of a third portion of benzoyl peroxide, but it has been exceptional that this has been required. Actually, all the various stages of polymerization can be obtained by use of a peroxide induced polymerization in a fourth or a third or in one-half the time required by air alone.

The final products obtained by these procedures varied from heavily viscous liquids to semi-rubbery or almost rubbery, or in fact, rubbe'ry solids or semi-solids which in each and every instance, were soluble in an organic solvent, as previously described. Needless to say, oxidation can be conducted in any convenient size reaction vessel; in fact, in a flask smaller than a 3-liter flask. This size is used simply as a matter of convenience.

I have previously pointed out that the products so obtained have utility for processes other than being subjected to oxyalkylation.

The polymerized derivatives above were subjected to oxalkylation by means of the various alkylene oxides previously described. The equipment used and the procedure were the same as described above except in the following respect. In the oxyalkylation to produce the oxyalkylated resins which are subsequently hydrogenated, etc., the amount of alkylene oxide added per initial reactant. i. e., the product being subjected to oxyalkylation, was comparatively small. The amount of alkylene oxide was in the neighborhood of one to two moles per phenolic hydroxyl. For this reason, the reaction period was comparatively short, regardless of whether high temperature or low temperature oxyalkylationwas used. The expression high temperature refers to oxya'lkylation taking place at 150 to 200- C., or, in some instances, somewhat higher. The expression "low temperature oxyalkylat-ion refers to temperatures approximately that of the boiling point of water, for instance, to C.,with to C. as average, and perhaps as highas C. at times. Suitable equipment is :used to control the time period involved, 1. e., the speed of injecting the oxide, and also the maximum temperature, the. maximum pressure, etc. In the oxalkylations described above, in order to use acomparatively low temperature (110? to 120 C.), two additional control units were connected to the equipment.

In the present oxyalkylation process, the amount of alkylene oxide being added is compare atively large. for instance, an equal weight or twice the weight, three times the weight, several times the weight, or even more, based on the initial reactant. For this reason, the higher temperatures were employed and the low temperature controls previously referred to were disconnected. 'The process is comparatively simple; the polymer, either as such or diluted with xylene or other suitable solvent, if desired, is placed in the. autoclave along with a suitable amount of alkaline catalyst, usually sodium methylate. The equipment is flushed out with nitrogen, various controls set, and oxyalkylation proceeds in the conventional manner. The procedure will be illustrated by the following examples:

Example 1 500 grams of the polymer identified as Example 1e, preceding, were mixed with 500 grams of xylene and 10 grams of sodium methylate. The reaction vessel employed was a stainless steel autoclave, with the usual devices for heating, heatcontrol, stirrer, inlet, outlet, etc., which are conventional in this type of apparatus. The capacity of the autoclave was approximately 3%; liters. The stirrer was operated at approximately 300 R. P. M. There was charged into the autoclave the mixture previously referred to, i. e., the polymer, the solvent, and the catalyst. The auto clave was sealed, swept with nitrogen gas, and stirring started immediately and heat applied. The temperature was allowed to rise to approximately C. The automatic controls were set to stop the reaction at C. and also to stop the equipment in event the pressure got higher than 200 pounds per square inch. The amount of ethylene oxide added was 500 grams. The inlet speed was set so as to introduce this amount of oxide in 2 hours. The injection of the ethylene oxide was controlled so it would all be added in one hours time. An allowance was made for the fact that the pressure control or temperature control might stop the injection of ethylene oxide at various intervals during the addition of the oxide, and for this reason, a 2-hour time period was allowed for actual injection of the oxide, i. e., injection at the rate of 500 grams per hour, plus an added interruption period of an hour, plus a half-hour for stirring at the end of the reac-' tion. In actual operation, the oxide was added in slightly over an hour and thefinal period of stirring probably was considerably over an hour. This, of course, was purely a matter of conven- 23 ience and immaterial, for the reason that if the temperature had been raised; slightly, or the amount of catalyst increased, the reaction could have taken place in even a shorter period of No harm was 24 alkylation the amount of ethylene oxide indicated was replaced by 32 /270 more of propylene oxide. In some instances, the time required for oxypropylation was somewhat longer than for oxytime, for instance, 45 minutes. ethylation, and in some instances, the temperadone, of course, in extending the period of reacture was slightly higher, 5 C. to 12 C., for extion, and likewise, no harm was done in having ample. The former insoluble product, after the a longer stirring period during the reaction to second stage of oxypropylation, was then treated insure there was no trace of ethylenet oxide left. with ethylene oxide in the same manner noted During this time the temperature did reach the in the previous table. If the product did not maximum point, i. e., 165, but the pressure did happen to'be water-soluble or sufficiently waternot go higher than 17 0 pounds per square inch. soluble, a fourth oxypropylation was employed,

The resultant Product W a light a ber Oil using about 25% of the amount of ethylene oxwhich dispersed readily in water either in preside previously noted. This second addition of ence of xylene or af er t e y e was e ov ethylene oxide and four oxyalkylations invariably This O y y fl Product Was j ed to produced water-solubility. Note what has been ther oxyethylation in the same mannenas noted said previously that water-solubility per se is not in t e acw pa y liable under Example fa criterion of efiective demulsifying action. It The example identified as f In the table was does, however, frequently characterize a waterthen subjected to a third stage of y t y a o soluble, surface-active material suitable for puras noted under Example 3 in the table. Various poses th th demu15ification e n u t in he same other oxyethylat1ons w re co (1 0 ed t Example manner under substantially the same operatin conditions. Such data are recorded in the table The same piece of equipment was used as preimmediately following: 25, viously described, 1. e., an autoclave, although in 1 Amt. ADD- Solvent Sod Max- 'r k ETO Tem Rat1o ,Ex. Derive- 5 Present Methyl Added Time Pres.lbs ETO to Solubility inwater No. two No. (S01Vent Grins. ate Add- Grms (Hours) per sq. Polymer I Ire (Xylene) ed Grms v in by Wt.

1e 500 500 10 I 500 3 165 170 1:1 Emuls. 0r sol. 1] 1,000 500 5 510 4 178 145 2:1 Increased sol 2] 1,510 500 0 550 414 180 170 3:1 Excel. sol. 2e 505 510 11 505 3% 170 185 1:1 Emuls. or sol. 4 r 1,010 510 5 I 520 3% 170 21 Increased 51' 1, 530. 510 -7 V 500, 4 185 100 5:1 1211551501. 3e 495 485 10 520 4 155 150 1:1 Emuls. or sol. 11 1,015 455 4 510 '4 154 150 2:1 Incr. sol. 8 1,525 485 5 490 3 109 150 311 Excel. sol. 70 503 49s 12 495 3 150 150 11 Emuls. or sol. 10] 99s 49s 5 400 a 151 180 21 111515.551. ll] 1, 488 49s 5 525 4% 158 175' 3:1 Excel. s01. 500 510 0 490 a 185 1'15 11 Emuls. or sol. 13 900 510 5 520 5 170 2=1 Incr. sol. 14; 1,510 510 5 '3 540 4 105 3:1 Excel. 801.

54 505 515 10 515 4 105 1:1 Emuls. or sol. 16] 1,020 515 7 500 4 105 155 211 ID011501- 171 1,520 515 5 505 3 ,5 150 311 Excel. s01.

62 520 505 10 510 3 ,5 145 100 11 Emuls. or sol. 19 1, 030 505 0 490 4 5 155 110 21 Incr. sol. '20; 1,520 505 5 v520 4 155 180 5:1 Excel. sol.

Example 22 Propylene oxide was used instead of ethylene oxide, following the same procedure as in Examples 1 through 21 preceding, but with this particular change: the amount of propylene oxide added was reversed roughly in molar proportion, i. e., approximately 13 A- grams of' propylene oxide were used to replace each 10 grams of ethylene oxide. Propylene oxide did not produce equivalent water-solubility even at the ultimate stages, or even when used in a greater amount. For this reason it is my preferenceto use propylene oxide in combination with either ethylene oxide or glycide, or both. It is understood that water-solubility may be particularly desirable to produce a surface-active agent, but fwatersolubility is not necessarily the criterion'of an efi'ec tive demulsifier. Indeed, some of the water-insoluble compounds obtained with propylene oxide appear to be as good demulsifiers as the more water-soluble ones obtained in a mixture of alkylene oxide as described in the next'succeeding paragraph.

In one modification the procedure followed was the same as in Examples 1; through 21f, but with. this difference; in the first two stages of oxy-' the instant experiment involving the use of gly- I funnel and an equalizing pressure tube so that. liquid, such as glycide, could be fed continuously at a drop-wise or a faster rate into the vessel, and

the rate was controlled by visual examination. For convenience, this piece of equipment is referred to as an autoclave because it was designed essentially for such use, but it is to be noted that,

it was not so used when glycide was employed as an alkylene oxide.

There were charged into the autoclave the same reactants (intermediate, solvent, and sodium methylate) as in Example 1f. The autoclave was sealed, swept with nitrogen gas and stirring started immediately and heat applied. The temperature was allowed to rise to 118 C. The glycide employed was comparatively pure. 360

grams of glycide were used. This was charged into the upper reservoir vessel which had been previously flushed out with nitrogen and was the equivalent of a separatoryi funnel. The glycide was started slowly into the reaction mass in a dropwise stream. The reaction started to take place immediately and the temperature rose approximately 10" to 15. Cooling water was run through the coils so that the temperature for addition of glycide was controlled within the range roughly of 110 to 130 C. The addition was continuous within the limitations and all the glycide was added in less than 7 hours. This reaction took place at atmospheric pressure, with simply a small stream of nitrogen passing into the autoclave at the very top, and passing out through the open condenser, so as to avoid any possible entrance of air. This amount of glycide gave the product reasonably good solubility. However, a second addition of glycide was made without adding more catalyst. The amount added the second time was 130 grams. This was added the same way in approximately a 3-hour period. This product showed moderately increased solubility over the previous sample. A third addition of oxide was made after first introducing an additional 5 grams of sodium methylate as catalyst. The third addition consisted of 250 grams of glycide. The product showed excellent solubility and excellent surface-active characteristics after the third addition of glycide. Note what has been said previously that watersolubility per se is not necessarily an index as to demulsification characteristics.

Oxyalkylated derivatives can be obtained without the use of a solvent as a diluent. This is purely a matter of convenience. Whichever solvent is used, such as xylene, cymene, decalin, or the like, can be removed by distillation, and particularly vacuum distillation. For many purposes, such as for use in demulsifiers, the solvent can remain.

It is my preference, particularly for purpose of demulsification, to use an oxyalkylated derivative which is surface-active by a simple emulsification test intended to produce a xylene-water emulsion. A suitable procedure is as follows: The oxyalkylated product is dissolved in an equal weight of xylene. Such 50-50 solution is then mixed with 1-3 volumes of water and shaken to produce an emulsion. The amount of xylene is invariably sufiicient to reduce even a tacky resinous product to a solution which is readily dispersible. The emulsions, so produced, are usually xylene-inwater emulsions (oil-in-water type) particularly when theamount of distilled water used is at least slightly in excess of the volume of xylene solution and also if shaken vigorously. At times, particularly in the lowest stage of oiq alkylation, one may obtain a water-in-xylene emulsion (water-in-oil type) which is apt to reverse on more vigorous shaking and further dilution with water.

If in doubt as to this property, comparison with a resin obtained from para-tertiary butylphenol and formaldehyde (ratio 1 part phenol to 1.1 formaldehyde) using an acid catalyst and then followed by oxyalkylation, using 2 moles of ethylene oxide for each phenolic hydroxyl, is helpful. Such resin, prior to oxyalkylation, has a molecular weight indicating about 4 units per resin molecule. Such resin, when diluted with an equal weight of xylene, will serve to illustrate the above emulsification test.

In a few instances the oxyalkylated product may not be sufficiently soluble in xylene alone, but may require the addition of some ethylene glycol diethylether as described elsewhere. It is understood that such mixture, or any other 26 imilar mixture, is considered the equivalent of xylene for the purpose of this test.

In many cases there is no doubt as to the presence or absence of hydrophile or surfaceaotive characteristics in the products used in accordance with this invention. They dissolve or disperse in water; and such dispersions foam readily. With borderline cases, i. e., those which show only incipient hydrophile or surface-active property (sub-surface-activity) tests for emulsifying properties of self-dispersibility are useful. The fact that a product is capable of producing a dispersion in water, is proof that it is distinctly hydrophile. In doubtful cases comparison can be made with the butylphenol-formaldehyde resin analogue, wherein 2 moles of ethylene oxide have been introduced for each phenolic nucleus. For more complete description of this test see U. S. Patent No. 2,499,370, dated March '7, 1950, to De Groote et al.

The presence of xylene or an equivalent waterinsoluble solvent may mask the point at which a solvent-free product on mere dilution in a test tube exhibits self -emulsification. For this reason, if it is desirable to determine the approximate point where self-emulsification begins, then it is better to eliminate the xylene or equivalent from a small portion of the reaction mixture and test such portion. In some cases such xylene-free resultant may show initial or incipient hydrophile properties, whereas, in presence of xylene such properties would not be noted. In other cases, the first objective indication of hydrophile properties may be the capacity of the material to emulsify an insoluble solvent such as xylene. It is to be emphasized that hydrophile properties herein referred to are such as those exhibited by incipient self-emulsification, or the presence of emulsifying properties and go through the range of homogeneous dispersibility or admixture with water, even in presence of added waterinsoluble solvent and minor proportions of common electrolytes as occur in oil field brings.

In summary, then, for all practical purposes oxyalkylations of the kind herein described are conducted in the conventional manner. The oxyalkylated derivatives, so obtained, are employed for the resolution of petroleum emulsions of the water-in-oil type. The oxyalkylated derivatives themselves may be used for a variety of purposes other than demulsification, where surface-active materials are of value, as, for example, producing emulsions, detergents, agricultural sprays, further reaction with chemical compound reactive towards hydroxyl radicals, etc.

Specifically, then, the use of such oxyalkylated derivatives is not limited to the resolution of petroleum emulsions of the water-in-oil type.

Conventional demulsifying agents employed in the treatment of oil field emulsions are used as such, or after dilution with any suitable solvent, such as water, petroleum hydrocarbons, such as benzene, toluene, xylene, tar acid oil, cresol, anthracene oil, etc. Alcohols, particularly aliphatic alcohols, such as methyl alcohol, ethyl alcohol, denatured alcohol, propyl alcohol, butyl alcohol, hexyl alcohol, octyl alcohol, etc., may be employed as diluents. Miscellaneous solvents, such as pine oil, carbon tetrachloride, sulfur dioxide extract obtained in the refining of petroleum, etc., may be employed as diluents. Similarly, the material or materials employed as the demulsifying agent of my process may be admixed with one or more of the solvents customarily used in connection with conventional demulsifying agents. Moreover, said material or materials may be used alone or in admixture with other suitable well known classes of demulsifying agents.

It is Well known that conventional demulsifying agents may be used in a Water-soluble form, or in an oil-soluble form, or in a form exhibiting both oiland water-solubility. Sometimes they may be used in a form which exhibits relatively limited oil-solubility. However, since such reagents are frequently used in a ratio of 1 to 10,000, or 1 to 20,000, or 1 to 30,000, or even 1 to 40,000, or 1 to 50,000 as in desalting practice, such an apparent insolubility in oil and water is not significant, because said reagents undoubtedly have solubility within such concentrations. This same fact is true in regard to the material or materials employed as the demulsifying agent of my process.

In practising my process for resolving petroleum emulsions of the water-in-oil type, a treating agent or demulsifying agent of the kind above described is brought into contact with or caused to act upon the emulsion to be treated, in any of the various apparatus now generally used to resolve or break petroleum emulsions with a chemical reagent, the above procedure being used alone or in combination with other demulsifying procedure, such as the electrical dehydration process.

One type of procedure is to accumulate a volume of emulsified oil in'a tank and conduct a batch treatment type of demulsification procedure to recover clean oil. In this procedure the emulsion is admixed with the demulsifier, for example, by agitating the tank of emulsion and slowly dripping demulsifier into the emulsion. In some cases, mixing is achieved by heating the emulsion while dripping in the demulsifier, depending upon the convection currents in the emulsion to produce satisfactory admixture. In a third modification of this type of treatment, a circulating pump withdraws emulsion from, e. g. the bottom of the tank, and re-introduces it into the top of the tank, the demulsifier being added, for example, at the suction side of said circulating pump.

In a second type of treating procedure, the demulsifier is introduced into the well fluids at the well-head or at some point between the well-head and the final oil storage tank, by means of an adjustable proportioning mechanism or proportioning pump. Ordinarily, the flow of fluids through the subsequent lines and fittings suflices to produce the desired degree of mixing of demulsifier and emulsion, although in some instances, additional mixing devices may be introduced into the flow system. In this general procedure, the system may include various mechanical devices for withdrawing free water, separating entrained water, or accomplishing quiescent settling of the chemicalized emulsion. Heating devices may likewise be incorporated in any of the treating procedures described herein.

A third type of application (down-the-hole) of demulsifier to emulsion is to introduce the demulsifier either periodically or continuously in diluted or undiluted form into the well and to allow it to come to the surface with the well fluids, and then to flow the chemicalized emulsion through any desirable surface equipment, such as employed in the other treating procedures. This particular type of application is decidedly useful when the demulsifier is used in connection with acidification of calcareous oil-bearing strata,

employed for acidification.

In all cases, it will be apparent from the foregoing description, the broad process consists simply in introducing a relatively small proportion of demulsifier into a relatively large propor-- tion of emulsion, admixing the chemical and emulsion either through natural flow or through special apparatus, with or without the application of heat, and allowing the mixture to stand quiescent until the undesirable water content of the emulsion separates and settles from the mass.

The following is a typical installation:

A reservoir to hold the demulsifier of the kind described (diluted 0r undiluted) is placed at the well-head where the eilluent liquids leave the well. This reservoir or container, which may vary from 5 gallons to 50 gallons, for convenience, is connected to a proportioning pump which injects the demulsifier drop-wise into'the fluids leaving the well. Such chemicalized fluids pass through the flow-line into a settling tank. The settling tank consists of a tank of any convenient size, for instance, one which will hold amounts of fluid produced in 4 to 24 hours (500 barrels to 2,000 barrels capacity), and inwhich there is a perpendicular conduit fromthe top 01' the tank to almost the very bottom so as to'permit the incoming fluids to pass from the top oi'th'e settling tank to the bottom, so that such incoming fluids do not disturb stratification which takesplace during the course of demulsification. The settling tank has two outlets, one being below the water level to drain off the water resulting from demulsification or accompanying the emulsion as free water, the other being an oil outlet at the top to permit the passage of dehydrated oil to a second tank, being a storage tank, which holds pipeline or dehydrated oil. If desired, the conduit or pipe which serves to carry'the fluids from the well to the settling tank may include a section of pipe with baffles to serve as a mixer, to insure thorough distribution of the demulsifier throughout the fluids, or a heater for raising the temperature of the fluids to some convenient temperature, for instance, to F., or both heater and mixer.

Demulsiflcation procedure is started by simply setting the pump so as to feed a comparatively large ratio of demulsifier, for instance, 1:5,000. As soon as a complete Break or satisfactory demulsification is obtained, the pump is regulated until experience shows that the amount of demulsifier being added is just suflicient to produce clean or dehydrated oil. The amount being fed at such stage is usually 1:10,000, 1:15,000, 1 :20,000, or the like.

In many instances, the oxyalkylated products herein specified as demulsiflers can be conveniently used without dilution. However, as previously noted, they may be diluted as desired with any suitable solvent. For instance, by mixing 75 parts by weight of an oxyalkylated derivative, for example, the product of Example 2 with 15 parts by weight of xylene and 10 parts by weight of isopropyl alcohol, an excellent demulsifier is obtained. Selection of the solvent will vary, depending upon the solubility characteristics of the oxyalkylated product, and of course, will be dictateld, in part, by economic considerations, i. e.,' cos As noted above, the products herein described may be used not only in diluted form, but also may be used admixed with some other chemical demulsifier. A mixture which illustrates such combination is the following:

Oxyalkylated derivative, for example, the prodnot of Example 2 20 A cyclohexylamine salt of monosulfonic acid, 24%

An ammonium salt of a polypropylated naphthalene monosulfonic acid, 24

A sodium salt of oil-solubl mahogany petroleum sulfonic acid, 12%;

A high-boiling aromatic petroleum solvent, 15%

Isopropyl acohol, 5 i

The. above proportions are all weight percents.

Having thus described my invention, what I claim as new and desire to secure by Letters Patent is:

1'. A process for breaking petroleum emulsions of the water-in-oil type, characterized by subjecting. the emulsion to the action of a demulsifier including oxyalkylation products; said oxyalkylation products being obtained by a process of a polypropylated ta) Reacting a phenol with an-aldehyde so' as to yield (b) An oxyalkylation-susceptible, fusible, or ganic solvent-soluble, water-insoluble phenolaldehyde resin; said resin being derived. by reaction between a difunctional monohydric phenol and an aldehyde having not over 8 carbon atoms and reactive towards said phenol; said resin being formed in the substantial absence of trifunctional phenols; said phenol being of the formula radicals, butylene radicals, hydroxypropylene radicals, and hydroxybutylene radicals; with the proviso that from about one-half to less than two mols of alkylene oxide be introduced for each phenolic nucleus;

(d) Converting said oxyalkylated resin into the corresponding alicyclic compound by hydrogenation in presence of a hydrogenating catalyst;

(e) Reacting said alicyclic compound with allyl glycidyl ether, with the proviso that at least 2 moles of allyl glycidyl ether be reacted for each alicyclic resin molecule and not in excess of three moles of allyl glycldyl ether per hydroxyl radical present in said molecule;

(f) Polymerizing said allyl radical-containing derivative to yield an organic solvent-soluble product; and

(g) subjecting said aforementioned polymer to oxyethylation with (h) An alpha-beta alkylene oxide having not more than 4 carbon atoms and selected from the class consisting of ethylene oxide, propylene oxide, butylene oxide, glycide and methylglycide; said oxyalkylated resin polymer being characterized by the introduction into the resin polymer molecule, of a plurality of divalent radicals having the formula (B10), in which R1 is a member selected from the class consisting of ethylene radicals, propylene radicals, butylene radicals, hydroxylpropylene radicals, and hydroxybutylene radicals.

2. A process for breaking petroleum emulsions of the water-in-oil type, characterized by subjecting the emulsion to the action of a demulsifier including oxyalkylation products; saidoxyalkylation products being obtained by a process of (a) Reacting a phenol with an aldehyde so as to yield (b) An' oxyalkylation-susceptible, fusible, organic solvent-soluble, water-insoluble phenolaldehyde'resin; said resin being derived-by reaction between. a difunctional monohydric phenol and an aldehyde having not over 8 carbonlatoms andf'reactive towards said phenol; said resin being formed in the substantial absence of trifunctional phenols; said phenol being of the formula in which R is a hydrocarbon radical having at least 4 and not more than 18 carbon atoms and substituted in the 2,4,6 position; subjecting said aforementioned resin to oxyalkylation with (-0) An alpha-beta alkylene oxide having not more than 4 carbon atoms and selected from the class consisting of ethylene oxide, propylene oxide, butylene oxide, glycide and methylglycide; said. oxyalkylated, resin being characterized by the introduction into the resin molecule of '-a plurality of divalent radicals having the formula R10, in which R1 is a member selected from the classconsistingof ethylene radicals, propylene radicals, butylene radicals, hydroxypropylene radicals, and hydroxy-butylene radicals; with the proviso that from about one-half to less than two moles of alkylene oxide be introduced for each phenolic nucleus;

(01) Converting said oxyalkylated resin into the corresponding alicyclic compound by hydrogenation in presence of a hydrogenating catalyst;

(e) Reacting said alicyclic compound with allyl glycidyl ether, with the proviso that at least 2 moles of allyl glycidyl ether be reacted for each alicyclic resin molecule and not in excess of three moles of allyl glycidyl ether per hydroxyl radical present in said molecule;

(1) Polymerizing said allyl radical-containing derivative to yield an organic solvent-soluble product;

(g) subjecting said aforementioned polymer to oxyethylation with (it) An alpha-beta alkylene oxide having not I more than 4 carbon atoms and selected from the class consisting of ethylene oxide, propylene oxide, butylene oxide, glycide and methylglycide; said oxyalkylated resin polymer being The process of claim 2, wherein the aldehyde is formaldehyde and the alkylene oxide is ethylene oxide.

5. The process of claim 2, wherein the aldehyde is formaldehyde and the alkylene oxide is ethylene oxide, with the proviso that in the (c) section, the molal ratio of ethylene oxide to initial phenolic hydroxyl be approximately 1 to 1. 6. The process of claim 2, wherein the aldehyde is formaldehyde and the alkylene oxide is ethylene oxide, with the proviso that in the (c) section, the molal ratio of ethylene oxide to initial phenolic hydroxyl be approximately 1 to 1; and with the further proviso that the molal ratio of allyl glycidyl ether to the corresponding alicyclic hydroxyl be approximately 1 to 1.

7. The process of claim 2, wherein the aldehyde is formaldehyde and the alkylene oxide is ethylene oxide, with the proviso that in the (c) section, the molal ratio of ethylene oxide to initial phenolic hydroxyl be approximately 1 to 1, and with the further proviso that the molal ratio of allyl glycidyl ether to the corresponding alicyclic hydroxyl be approximately 1 to 1; and with the final proviso that the radical R is a butyl radical.

8. The process of claim 2, wherein the aldehyde is formaldehyde and the alkylene oxide is ethylene oxide, with the proviso that in the (c) section, the molal ratio of ethylene oxide to initial phenolic hydroxyl be approximately 1 to 1, and with the further proviso that the molal ratio of allyl glycidyl ether to the corresponding alicyclic hydroxyl be approximately 1 to 1; and with the final proviso that the radical R is an amyl 3 radical. v

V 9. The process of claim 2, wherein the aldehyde is formaldehyde and the alkylene oxide is ethylene oxide, with the proviso that .in the (0) section, the molal ratio of ethylene oxide to initial phenolic hydroxyl be approximately 1 to 1, and with the further proviso that the molal ratio of allyl glycidyl ether to the corresponding alicyclic hydroxyl be approximately 1 to 1; and with the final proviso that the radical R is an octyl radical.

10. The process of claim 1, wherein the aldehyde is formaldehyde and the alkylene oxide is ethylene oxide, with the proviso that in the (c) section the molal ratio of ethylene oxide to initial phenolic hydroxyl be approximately 1 to 1, and with the further proviso that the molal ratio of allyl glycidyl ether to the corresponding alicyclic hydroxyl be approximately 1 to 1; and with the final proviso that the radical R is a nonyl radical.

11. The process of claim 1, wherein the aldehyde is formaldehyde and the alkylene oxide is ethylene oxide, with the proviso that in the (c) section, the molal ratio of ethylene oxide to initial phenolic hydroxyl be approximately 1 to 1-, and with the further proviso that the molal ratio of allyl glycidyl ether to the corresponding alicyclic hydroxyl be approximately 1 to 1; and with the final proviso that the radical R is a tetradecyl radical.

- MELVIN DE GROOTE.

REFERENCES CITED The following references are of record in the file of this patent:

UNITED sT TEs PATENTS Wiles Nov. '7, 1950 

1. A PROCESS FOR BREAKING PETROLEUM EMULSIONS OF THE WATER-IN-OIL TYPE, CHARACTERIZED BY SUBJECTING THE EMULSION TO THE ACTION OF A DEMULSIFIER INCLUDING OXYALKYLATION PRODUCTS; SAID OXYALKYLATION PRODUCTS BEING OBTAINED BY A PROCESS OF (A) REACTING A PHENOL WITH AN ALDEHYDE SO AS TO YIELD (B) AN OXYALKYLATION-SUSCEPTIBLE, FUSIBLE, ORGANIC SOLVENT-SOLUBLE, WATER-INSOLUBLE PHENOLALDEHYDE RESIN; SAID RESIN BEING DERIVED BY REACTION BETWEEN A DIFUNCTIONAL MONOHYDRIC PHENOL AND AN ALDEHYDE HAVING NOT OVER 8 CARBON ATOMS AND REACTIVE TOWARDS SAID PHENOL; SAID RESIN BEING FORMED IN THE SUBSTANTIAL ABSENCE OF TRIFUNCTIONAL PHENOLS; SAID PHENOL BEING OF THE FORMULA 